EP1205442A1 - Verfahren zur Trennung von Gas, Wasser und Biomasse und Dreiphasentrennsystem - Google Patents

Verfahren zur Trennung von Gas, Wasser und Biomasse und Dreiphasentrennsystem Download PDF

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Publication number
EP1205442A1
EP1205442A1 EP00124408A EP00124408A EP1205442A1 EP 1205442 A1 EP1205442 A1 EP 1205442A1 EP 00124408 A EP00124408 A EP 00124408A EP 00124408 A EP00124408 A EP 00124408A EP 1205442 A1 EP1205442 A1 EP 1205442A1
Authority
EP
European Patent Office
Prior art keywords
gas
phase separation
biogas
separation system
biomass
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP00124408A
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German (de)
English (en)
French (fr)
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
VA Tech Wabag Deutschland GmbH
Original Assignee
VA Tech Wabag Deutschland GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by VA Tech Wabag Deutschland GmbH filed Critical VA Tech Wabag Deutschland GmbH
Priority to EP00124408A priority Critical patent/EP1205442A1/de
Priority to PCT/EP2001/012673 priority patent/WO2002038509A1/de
Priority to EP01993587A priority patent/EP1337476A1/de
Priority to CNB018185223A priority patent/CN1240628C/zh
Priority to AU2002215997A priority patent/AU2002215997A1/en
Publication of EP1205442A1 publication Critical patent/EP1205442A1/de
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/18—Flow directing inserts
    • C12M27/20—Baffles; Ribs; Ribbons; Auger vanes
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/24—Recirculation of gas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M33/00—Means for introduction, transport, positioning, extraction, harvesting, peeling or sampling of biological material in or from the apparatus
    • C12M33/22—Settling tanks; Sedimentation by gravity
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the invention relates to a method for separating gas, water and biomass in one Sludge bed reactor according to the preamble of claim 1 and a three-phase separation system according to the preamble of claim 6.
  • organic wastewater constituents are agglomerated and fluidizable microorganisms cleaned.
  • the agglomerates of the biomass form - in a non-fluidized state - a sludge bed in the bottom area of the Reactor into which the wastewater to be treated is mixed.
  • sludge bed becomes biomass in the process retained and on the other hand treated wastewater and that during fermentation biogas formed is deducted separately from the process.
  • UASB-reactors U PFlow A naerobic S ludge lanket B
  • the waste water is mixed in such a reactor in the bottom area of the sludge bed.
  • a UASB reactor is known for example from EP 244 029 B1 or EP 808 805 A1.
  • the invention also relates to this type of reactor.
  • the biomass is usually in the form of a mixture in a sludge bed reactor which consists of spherical or ellipsoidal agglomerates of microorganisms and also composed of flaky fine sludge, the diameter of the agglomerates be around 1 - 5 mm.
  • precipitation products can also be used contribute to the construction of the agglomerates.
  • the density of the agglomerates is greater than that of the water, which is why it is formed by the Sedimentation from a sludge bed in the bottom area of the reactor. That when dismantling the Biogas produced from organic waste water constituents forms bubbles in the Move the mud bed upwards.
  • the bubbles initially adhere to the agglomerates, until they are sheared and / or sufficiently sized by them to solve.
  • the rate of ascent of the bubbles is determined by their size can also be determined by the pressure conditions in the bottom region of the reactor. All in all the bubble ascent rate is so high that the biomass is fluidized and can form a floating bed. This floating bed has a relatively smaller one Share of biomass than a sludge bed and thus takes up a larger volume one than this.
  • biogas From the added cargo of organic wastewater constituents, a certain one Amount of biogas are generated. Depending on the amount of biogas a certain part of the sludge bed is fluidized by the rising gas bubbles and is available as a floating bed, with a portion of the agglomerates additionally due to adherent Blowing up gas bubbles.
  • Sludge bed reactors contain three-phase separation systems with which biogas can be treated Have wastewater and biomass separated. Three-phase separation systems can be designed differently depending on the weighting of the different tasks his.
  • the biogas can either be contained in gas hoods or through baffles be derived to the reactor head. This ideally ensures that none Gas bubbles and no gas-laden sludge get into the area of the gutters.
  • the main task of all three-phase separation systems is to separate the phases to achieve as completely as possible.
  • the difficulty of good three-phase separation is particularly the agglomerates to separate from the adhering gas bubbles.
  • Specifically heavier agglomerates can just balance through the attachment of specifically lighter agglomerates be that the gaseous agglomerate, which in the surrounding water no up or Buoyancy forces are experienced, so to speak floating freely from the currents in the water becomes.
  • Such a gas-laden agglomerate can now deal with the flowing sewage the gas-repellent baffles get around in the area of the gutters and with the expiry will be carried out. This output can be removed by the previous separators cannot be avoided in a targeted manner.
  • the stripping of biomass should be avoided because on the one hand, drives off active biomass and, on the other hand, through the abrasive solids the subsequent treatment stages are unnecessarily burdened.
  • the gas separation can only take place with high efficiency if the medium one Rotation speed of the roller reaches a certain minimum speed. Since the The roller is driven directly by the ascent of the released biogas bubbles Coupled to the current load and dismantling situation. In principle can then the current roller speed can be assigned to three areas: 1. too slow with low biogas production, 2. in the right area with biogas production in Design range, 3. too fast with too high biogas production. Too high roller speed can lead to excessive shear stresses on the agglomerates. Then not only the adhering gas is separated, sometimes the agglomerates itself affected in such a way that they break partially or completely. Overall, development can be initiated through shear stresses of this type the larger, spherical agglomerates are disadvantaged and small-volume, flaky Agglomerates preferred.
  • Wastewater, especially industrial wastewater, is subject to changes over time Composition marked.
  • the compositions are in the industrial field through daily and weekly working hours, cleaning intervals and also campaign operations embossed. There is also a medium-term burden in the design area characterized by hourly or daily under or overloading.
  • the previously known process technology can only insufficient react.
  • the recirculation can be increased to less hydraulic load to increase the inflow speed.
  • An object of the present invention is now a method and a corresponding one To create three-phase separation system, where even with different loads there is sufficient separation of biogas and agglomerates and thus an improved process quality is achieved.
  • the rotational speed of the liquid roller of the method according to the invention be influenced so that the speed of rotation increases with low gas production as well as the rotational speed is reduced with high gas production.
  • the Liquid roller prevents a gas siphoning effect over the stack of plates formed.
  • gas in particular biogas
  • a side of the Plate stack arranged gas bubbling are passed. There it rises and accelerates the liquid roller lying horizontally above it.
  • a flow wedge located on the underside of the lower plate acts as a stall edge and stabilizes the horizontal liquid roller so that that all plates are used better hydraulically.
  • the direction of rotation of the liquid roller is due to the combination of gas introduction and flow separation edge stabilizes and beats even under different load conditions Not about.
  • control of the rotational speed of the liquid roller is dispensed with and therefore only by means of a stack of plates and a flow separation edge without the introduction of gas the desired effect can be achieved.
  • the introduced biogas either comes from the reactor head and is replaced by a corresponding one Pump pumped, it can be from separate containers or storage containers , e.g. Nitrogen can be used if not enough Biogas is available.
  • biogas is formed under the gas hood in the lower part of the three-phase separation system. This can either be done directly in the reactor head are derived, or via appropriate position of the valves in the Gas bubbling can be conducted. When feeding gas bubbling, the roller speed accelerated in the manner described above.
  • the retention of the biomass achieved under different load conditions.
  • significant A part of the biogas formed is drawn off or the separator added.
  • the remaining biogas rises freely outside of the separator (s) Water surface and collects in the area of the reactor head.
  • Fig. 1 shows a side view of a three-phase separation system, in the following briefly separator.
  • Fig. 2 shows the separator from Fig. 1 with vertical internals above the plate stack.
  • FIG. 3 shows the separator from FIG. 2 with further flow-directing devices over the stack of plates.
  • the separator is arranged in a closed reactor 1 and essentially consists from a gas hood 2, from plate stacks 3, from separator plates 4 and from Troughs 5.
  • a gas hood 2 Above the gas hood 2 are two plate stacks 3 each consisting of three Plates 6, 7, 8 arranged so that the liquid rising next to the gas hood 2 meets the bottom plate 6, rises along it and is deflected at its upper edge is and flows down along the plates 6, 7, 8 or the gas hood 2.
  • the separator plates 4 are arranged so that their upper end above the water level 9 of the sludge bed reactor 1 protrudes.
  • a flow wedge 10 is arranged on the lower plate 6 and works as a tear-off edge and thus brings about better hydraulic utilization of the plate stack 3.
  • the separator plates 4 arranged between the two plate stacks 3 form one open, flow - free, wedge - shaped separation space below, into which the water from enters below.
  • the troughs 5 on the water surface are arranged in such a way that the purified water collects and can be drained off.
  • a partition 20 can be provided about the currents in the separation room to separate.
  • the biogas produced in the reactor 1 is partly collected in the gas hood 2, whereby the water level 21 in the gas hood adjusts itself according to the amount of gas.
  • the Biogas is withdrawn via line 12 and can either be via line 18, valve 16 and line 17 are led through outlet 11 into the reactor head, the withdrawn The amount of gas is adjustable.
  • line 18, valve 15, line 19 and finally line 13 (the gas bubbling) the biogas specifically to increase the Rotational speed of the liquid roller are introduced, the supplied The amount of gas is also adjustable.
  • the liquid roller if not sufficient biogas is available, gas from a valve 14 and line 19 other source.
  • At least one device 24 for discharging the generated biogas is in the reactor head intended.
  • the separator is made up of straight elements, apart from the lines Extend normally to the drawing plane. Multiple lines are normal to the drawing level 13 arranged so that their gas outlets lie on straight lines and a linear Allow gas to be applied. The outlets of line 13 are close to the Reactor wall 1.
  • one or more separators on the water surface can be arranged parallel to this.
  • the invention takes advantage of the fact that agglomerates and adherent gas bubbles in one highly turbulent flow due to their difference in density and the differences resulting therefrom attacking acceleration forces can be separated.
  • the plate stack is used only for flow guidance, the flow through the stack is from top down. A certain proportion of the emerging flow flows into the calm one The end zone. Part of the flow is around the plate stack on a circular path again led up and for the most part plunges back into the plate stack.
  • the plate stack has no function with regard to possible sedimentation.
  • the separator according to the invention is designed so that it is located next to or above the Plate stack around a roller is developed and stabilized. Through further installations, which are structurally assigned to the stack of plates can support the formation of the roller become. If structural components are not installed according to the invention, the formation of rolls can occur disturb and possibly even prevent.
  • FIG. 2 shows, starting from FIG. 1, above the plate stack 3, aligned with the upper edge the outer or lower plate 6, each a further vertically arranged flat plate 22, which has the function of stabilizing the core of the roller.
  • Fig. 3 shows, starting from Fig. 2 above the plate stack 3, another flow-directing Means 23 which is triangular in cross section and has the function of ascending Feed gas bubbles and outflowing water to the roller in the direction of its rotation.

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  • Life Sciences & Earth Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Microbiology (AREA)
  • Genetics & Genomics (AREA)
  • General Engineering & Computer Science (AREA)
  • Biochemistry (AREA)
  • Sustainable Development (AREA)
  • General Health & Medical Sciences (AREA)
  • Biotechnology (AREA)
  • Biomedical Technology (AREA)
  • Molecular Biology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
  • Treatment Of Sludge (AREA)
EP00124408A 2000-11-08 2000-11-08 Verfahren zur Trennung von Gas, Wasser und Biomasse und Dreiphasentrennsystem Withdrawn EP1205442A1 (de)

Priority Applications (5)

Application Number Priority Date Filing Date Title
EP00124408A EP1205442A1 (de) 2000-11-08 2000-11-08 Verfahren zur Trennung von Gas, Wasser und Biomasse und Dreiphasentrennsystem
PCT/EP2001/012673 WO2002038509A1 (de) 2000-11-08 2001-11-02 Verfahren zur trennung von gas, wasser und biomasse und dreiphasentrennsystem
EP01993587A EP1337476A1 (de) 2000-11-08 2001-11-02 Verfahren zur trennung von gas, wasser und biomasse und dreiphasentrennsystem
CNB018185223A CN1240628C (zh) 2000-11-08 2001-11-02 分离气体、水和生物体的方法和三相分离系统
AU2002215997A AU2002215997A1 (en) 2000-11-08 2001-11-02 Method for separating gas, water and biomass and three-phase separating system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP00124408A EP1205442A1 (de) 2000-11-08 2000-11-08 Verfahren zur Trennung von Gas, Wasser und Biomasse und Dreiphasentrennsystem

Publications (1)

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EP1205442A1 true EP1205442A1 (de) 2002-05-15

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EP00124408A Withdrawn EP1205442A1 (de) 2000-11-08 2000-11-08 Verfahren zur Trennung von Gas, Wasser und Biomasse und Dreiphasentrennsystem
EP01993587A Withdrawn EP1337476A1 (de) 2000-11-08 2001-11-02 Verfahren zur trennung von gas, wasser und biomasse und dreiphasentrennsystem

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EP01993587A Withdrawn EP1337476A1 (de) 2000-11-08 2001-11-02 Verfahren zur trennung von gas, wasser und biomasse und dreiphasentrennsystem

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EP (2) EP1205442A1 (zh)
CN (1) CN1240628C (zh)
AU (1) AU2002215997A1 (zh)
WO (1) WO2002038509A1 (zh)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100506721C (zh) * 2006-07-20 2009-07-01 清华大学 提高折流式厌氧生物反应器三相分离效率的装置
CN100518878C (zh) * 2006-02-09 2009-07-29 财团法人工业技术研究院 三相分离装置
DE102008017020A1 (de) * 2008-04-03 2009-10-08 Wolfgang Eggert Reaktor mit Dreiphasentrennvorrichtung
CN102123776A (zh) * 2008-08-12 2011-07-13 沃依特专利有限责任公司 三相多级分离装置
CN108165473A (zh) * 2018-03-12 2018-06-15 王东霞 一种三相分离式沼气发生装置
CN112010426A (zh) * 2020-08-24 2020-12-01 苏州恺利尔环保科技有限公司 新型立式厌氧反应器

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4720709B2 (ja) * 2005-11-07 2011-07-13 栗田工業株式会社 生物反応器
NL2002207C2 (en) * 2008-11-13 2010-05-17 Haskoning Nederland B V Upflow anaerobic sludge blanket reactor.
CN101475261B (zh) * 2009-01-19 2011-01-26 浙江大学 一种用于污水厌氧生化反应器的三相分离器
CN106984068A (zh) * 2017-05-11 2017-07-28 江苏海澜正和环境科技有限公司 一种三相分离器
CN110002593B (zh) * 2019-05-08 2024-04-26 杭州师范大学 一种一体化分散式生活污水处理装置
CN111470623A (zh) * 2020-04-30 2020-07-31 上海复森环境科技发展有限公司 一种膜藕上流式厌氧污泥床反应器系统

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0808805A1 (de) * 1996-05-22 1997-11-26 CT Umwelttechnik AG Verfahren und Reaktor zur anaeroben Abwasserreinigung in einem Schlammbett
DE19815616A1 (de) * 1998-04-07 1999-10-14 Zeppelin Silo & Apptech Gmbh Verfahren und Vorrichtung zum Reinigen von Abwasser

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0808805A1 (de) * 1996-05-22 1997-11-26 CT Umwelttechnik AG Verfahren und Reaktor zur anaeroben Abwasserreinigung in einem Schlammbett
DE19815616A1 (de) * 1998-04-07 1999-10-14 Zeppelin Silo & Apptech Gmbh Verfahren und Vorrichtung zum Reinigen von Abwasser

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100518878C (zh) * 2006-02-09 2009-07-29 财团法人工业技术研究院 三相分离装置
CN100506721C (zh) * 2006-07-20 2009-07-01 清华大学 提高折流式厌氧生物反应器三相分离效率的装置
DE102008017020A1 (de) * 2008-04-03 2009-10-08 Wolfgang Eggert Reaktor mit Dreiphasentrennvorrichtung
CN102123776A (zh) * 2008-08-12 2011-07-13 沃依特专利有限责任公司 三相多级分离装置
CN102123776B (zh) * 2008-08-12 2014-05-28 沃依特专利有限责任公司 三相多级分离装置
CN108165473A (zh) * 2018-03-12 2018-06-15 王东霞 一种三相分离式沼气发生装置
CN112010426A (zh) * 2020-08-24 2020-12-01 苏州恺利尔环保科技有限公司 新型立式厌氧反应器
CN112010426B (zh) * 2020-08-24 2022-04-15 苏州恺利尔环保科技有限公司 立式厌氧反应器

Also Published As

Publication number Publication date
AU2002215997A1 (en) 2002-05-21
WO2002038509A1 (de) 2002-05-16
CN1240628C (zh) 2006-02-08
CN1473136A (zh) 2004-02-04
EP1337476A1 (de) 2003-08-27

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